Polymerization of α-olefins with transition metal catalysts based on bidentate ligands containing pyridine or quinoline moiety

ABSTRACT

Disclosed is a novel bidentate pyridine transition metal catalyst having the general formula ##STR1## where Y is O, S, NR, ##STR2## each R is independently selected from hydrogen or C 1  to C 6  alkyl, each R&#39; is independently selected from C 1  to C 6  alkyl, C 1  to C 6  alkoxy, C 6  to C 16  aryl, halogen, or CF 3 , M is titanium, zirconium, or hafnium, each X is independently selected from halogen, C 1  to C 6  alkyl, C 1  to C 6  alkoxy, or ##STR3## L is X, cyclopentadienyl, C 1  to C 6  alkyl substituted cyclopentadienyl, indenyl, fluorenyl, or ##STR4## and &#34;n&#34; is 1 to 4. Also disclosed is a method of making a poly-α-olefin comprising polymerizing an α-olefin monomer using that catalyst or a catalyst that has the general formula ##STR5## where Y, M, L, X, and R&#39; were previously defined.

BACKGROUND OF THE INVENTION

This invention relates to catalysts useful in polymerizing α-olefins. In particular, it relates to the polymerization of ethylene using transition metal catalysts with bidentate ligands containing pyridine or quinoline moieties.

Until recently, polyolefins have been made primarily using conventional Ziegler catalyst systems. A Ziegler catalyst typically consists of a transition metal-containing compound and one or more organometallic compounds. For example, polyethylene has been made using Ziegler catalysts such as titanium trichloride and diethylaluminum chloride, or a mixture of titanium tetrachloride, vanadium oxytrichloride, and triethylaluminum. These catalysts are inexpensive but they have low activity and therefore must be used at high concentrations. The catalyst residue in the polymers produces a yellow or grey color and poor ultraviolet and long term stability, and chloride-containing residues can cause corrosion in polymer processing equipment. It is therefore sometimes necessary to either remove catalyst residues from the polymer or add neutralizing agents and stabilizers to the polymer to overcome the deleterious effects of the residues and this adds to production costs. Furthermore, Ziegler catalysts produce polymers having a broad molecular weight distribution, which is undesirable for some applications, such as injection molding. They are also poor at incorporating α-olefin co-monomers, making it difficult to control polymer density. Large quantities of excess co-monomer may be required to achieve a certain density and many higher α-olefins, such as 1-octene, can be incorporated at only very low levels, if at all.

Although substantial improvements in Ziegler catalyst systems have occurred since their discovery, these catalysts are now being replaced with recently discovered metallocene catalyst systems. A metallocene catalyst typically consists of a transition metal compound that has one or more cyclopentadienyl ring ligands. Metallocenes have low activities when used with organometallic compounds, such as aluminum alkyls, which are used with traditional Ziegler catalysts, but very high activities when used with aluminoxanes as cocatalysts. The activities are generally so high that catalyst residues need not be removed from the polymer. Furthermore, they produce polymers with high molecular weights and narrow molecular weight distributions. They also incorporate α-olefin co-monomers well.

However, at higher temperatures metallocene catalysts tend to produce lower molecular weight polymers. Thus, they are useful for gas phase and slurry polymerizations of ethylene, which are conducted at about 80° C. to about 95° C., but in general they do not work well as temperatures are increased. The polymerization of ethylene in solution at higher temperatures is desirable because it allows great flexibility for producing polymers over a wide range of molecular weights and densities as well as the use of a large variety of different co-monomers. Solution polymerization permits the production of polymers that are useful in many different applications. For example, both high molecular weight, high density polyethylene (PE) film useful as a barrier film for food packaging and low density ethylene co-polymers with good toughness and high impact strength can be made.

SUMMARY OF THE INVENTION

We have discovered novel bidentate pyridine transition metal compounds which have excellent activity as α-olefin polymerization catalysts. We have also discovered that bidentate quinoline transition metal compounds, which were heretofore unsuspected of possessing any catalytic properties, are also excellent polymerization catalysts for α-olefins. These catalysts produce polymers having properties very close to the properties of polymers produced using metallocene catalysts. That is, the polymers have a narrow molecular weight distribution and a uniform co-monomer incorporation.

DESCRIPTION OF THE PREFERRED EMBODIMENTS

The transition metal catalysts of this invention containing the bidentate pyridine based ligand have the general formula ##STR6## where Y is O, S, NR, ##STR7## each R is independently selected from hydrogen or C₁ to C₆ alkyl, each R' is independently selected from R, C₁ to C₆ alkoxy, C₆ to C₁₆ aryl, halogen, or CF₃, M is titanium, zirconium, or hafnium, each X is independently selected from halogen, C₁ to C₆ alkyl, C₁ to C₆ alkoxy, or ##STR8## L is X, cyclopentadienyl, C₁ to C₆ alkyl substituted cyclopentadienyl, indenyl, fluorenyl, or ##STR9## and "n" is 1 to 4.

In the formula, the Y group is preferably oxygen as those compounds are easier to make. For the same reason the R group is preferably methyl and R' is preferably hydrogen. The L group is preferably halogen, most preferably chlorine, as those catalysts give superior properties and are easier to prepare. For the same reasons, the X group is preferably halogen, especially chlorine, and the M group is preferably titanium.

Preparation of the bidentate pyridine complexes is illustrated in the examples, but generally they can be prepared by reacting a substituted pyridine precursor having an acidic proton with a compound having the formula MX₃ L in the presence of an HX scavenger. The reaction is stoichiometric and stoichiometric amounts of scavenger are preferred. Examples of suitable scavengers include compounds that are more basic than the substituted pyridine, such as triethylamine, pyridine, sodium hydride, and butyl lithium. If the scavenger is a stronger base than the substituted pyridine one can make a salt of the substituted pyridine and begin with that. While the reaction is preferably performed in a solvent, only partial solubility of the reactants is required. An aprotic solvent, such as tetrahydrofuran (THF), ether, toluene, or xylene, can be used at about 0.2 to about 20 wt % solids, and preferably at about 5 to about 10 wt % solids. The reaction can occur at about -78° C. to about room temperature. As the reaction proceeds, a precipitate is formed and the product can be extracted with toluene, methylene chloride, diethyl ether, or a similar extractant.

The bidentate quinoline transition metal catalysts of this invention have the general formula ##STR10## where R, R', L, M, X, and "n" were previously defined.

The quinoline transition metal catalysts are made in a similar manner to the pyridine transition metal catalysts except that one begins with a substituted quinoline such as 8-hydroxy quinoline (also known as 8-quinolinol) instead of the substituted pyridine. Also, butyl lithium can be used in a solvent to make the lithium salt of 8-hydroxy quinoline, which can also be used as the starting material.

Since the catalyst is normally used in conjunction with an organometallic co-catalyst, it is preferable to dissolve the catalyst in a solvent in which the co-catalyst is also soluble. For example, if methylaluminoxane (MAO) or polymethylaluminoxane (PMAO) is the co-catalyst, then toluene, xylene, benzene, or ethylbenzene could be used as the solvent. The preferred co-catalyst is MAO as it results in high activity and a polymer having a narrower molecular weight distribution. The mole ratio of the organometallic co-catalyst to catalyst when used in a polymerization is generally in the range 0.01:1 to 100,000:1, and preferably ranges from 1:1 to 10,000:1.

An alternative co-catalyst is an acid salt that contains a non-coordinating inert anion (see U.S. Pat. No. 5,064,802). The acid salt is generally a non-nucleophilic compound that consists of bulky ligands attached to a boron or aluminum atom, such as lithium tetrakis(pentafluorophenyl) borate, lithium tetrakis(pentafluorophenyl)aluminate, anilinium tetrakis(pentafluorophenyl)borate, and mixtures thereof. The anion which results when these compounds react with the catalyst is believed to be weakly coordinated to the metal-containing cation. The mole ratio of acid salt to catalyst can range from about 0.01:1 to about 1000:1, but is preferably about 1:1 to 10:1. While there is no limitation on the method of preparing an active catalyst system from the catalyst and the acid salt, preferably they are mixed in an inert solvent at temperatures in the range of about -78° C. to about 150° C. They can also be mixed in the presence of monomer if desired. The acid salt can be used in combination with the organometallic cocatalysts described earlier.

The catalyst and co-catalyst can be used on a support such as silica gel, alumina, silica, magnesia, or titania, but supports are not preferred as they may leave contaminants in the polymer. However, a support may be required, depending upon the process being utilized. For example, a support is generally needed in gas phase polymerization processes and slurry polymerization processes in order to control the particle size of the polymer being produced and in order to prevent fouling of the reactor walls. To use a support, the catalyst and co-catalyst are dissolved in the solvent and are precipitated onto the support material by, for example, evaporating the solvent. The co-catalyst can also be deposited on the support or it can be introduced into the reactor separately from the supported catalyst.

The catalyst is used in a conventional manner in the polymerization of olefinic hydrocarbon monomers. While unsaturated monomers, such as styrene, can be polymerized using the catalysts of this invention, it is particularly useful for polymerizing α-olefins such as propylene, 1-butene, 1-hexene, 1-octene, and especially ethylene.

The catalyst is also useful in a conventional manner for copolymerizing mixtures of unsaturated monomers such as ethylene, propylene, 1-butene, 1-hexene, 1-octene, and the like; mixtures of ethylene and di-olefins such as 1,3-butadiene, 1,4-hexadiene, 1,5-hexadiene, and the like; and mixtures of ethylene and unsaturated comonomers such as norbornene, ethylidene norbornene, vinyl norbornene, norbornadiene, and the like.

The catalysts of this invention can be utilized in a variety of different polymerization processes. They can be utilized in a liquid phase polymerization process (slurry, solution, suspension, bulk phase, or a combination of these), in a high pressure fluid phase, or in a gas phase polymerization process. The processes can be used in series or as individual single processes. The pressure in the polymerization reaction zones can range from about 15 psia to about 50,000 psia and the temperature can range from about -78° C. to about 300° C.

EXAMPLE 1 Synthesis of Bis(2-pyridinoxy)titanium Dichloride

To a solution of 0.02 moles of 2-hydroxy pyridine and 0.02 moles of triethylamine in 50 mL of THF, a solution of 0.01 moles of titanium tetrachloride was added dropwise at 0° C. and stirred overnight at room temperature. After filtration, the THF solution was evaporated and the product was extracted from the residue. The product has the formula: ##STR11##

EXAMPLE 2 Preparation of (Cyclopentadienyl) (2-Pyridinoxy) Titanium Dichloride

To a solution of 0.002 moles of cyclopentadienyl titanium trichloride in 50 mL of ether a solution of 2-hydroxy pyridine (0.002 moles) and triethylamine (0.002 moles) in 50 mL of ether was added at 0° C. and stirred overnight. The product was recovered from the ether filtrate. The product has the formula: ##STR12##

EXAMPLE 3 General Procedure For Preparation of Quinolinoxy Transition Metal Catalysts

Toluene slurries of lithium salts of various 8-quinolinol derivatives (prepared using butyl lithium) were combined with the corresponding titanium or zirconium compound (titanium tetrachloride, zirconium tetrachloride, cyclopentadienyl titanium trichloride, or cyclopentadienyl zirconium trichloride) at -78° C. and stirred overnight at room temperature. The complexes were recovered from the reaction mixture by extraction with toluene or methylene chloride. To prepare 8-quinolinoxy titanium trichloride (III), ##STR13## a slurry of 0.01 moles of the lithium salt of 8-hydroxyquinoline in 30 ml of toluene (prepared from 1.45 g (0.01 moles) of quinolinol and MeLi) was added at -78° C. to a solution of 1.9 g (0.01 moles) of TiCl₁₄ in 20 ml of toluene and stirred overnight at room temperature. The precipitate was separated, washed with toluene, and extracted with 100 ml of CH₂ Cl₂. After the methylene chloride had been removed, a brown microcrystalline solid (0.7 g) was isolated.

Similarly, 8-(2-methyl-5,7-dichloroquinolin)oxytitanium trichloride (IV) (2.3 g) ##STR14## was prepared starting with a lithium salt made from 2.28 g (0.01 moles) of 5,7-dichloro-2-methyl-8-quinolinol.

A similar procedure was used to prepare 1.0 g of the comparative complex bis[8-(2-methyl-5,7-dichloroquinolin)oxy]zirconiumdichloride (V) ##STR15## from 2.28 g (0.01 moles) of 5,7-dichloro-2-methyl-8-quinolinol and 1.165 g (0.005 moles) of zirconium tetrachloride.

To prepare (cyclopentadienyl)-(8-quinolinoxy)zirconium dichloride (VI) ##STR16## and (cyclopentadienyl) -[8-(2-methyl-5,7-dichloroquinolin)oxy]zirconium dichloride (VII) ##STR17## lithium salts made from 1.45 g (0.01 moles) of 8-quinolinol or 1.15 g (0.005 moles) of 5,7-dichloro-2-methyl-8-quinolinol, respectively, were reacted with equimolar amounts of cyclopentadienyl zirconium trichloride in toluene at -78° C. After stirring overnight and filtering, the products (0.62 g of VI and 1.7 g of VII) were isolated from the toluene solution.

EXAMPLE 4 Polymerizations

All polymerizations in this study were conducted in a 1.7 L reactor. Prior to conducting a polymerization, the reactor was "baked-out" by heating to 130° C. and holding at that temperature for 30 minutes under a nitrogen purge. Ethylene, hydrogen, hexene, butene, and nitrogen were treated by passage through columns containing 13X molecular sieves. For a typical polymerization, the reactor was charged with 0.850 L of hexane or toluene and, using a syringe, the required volume of diluted PMAO (AKZO). The desired amount of hydrogen was added to the reactor by monitoring the pressure drop (ΔP) from a 1 L stainless steel vessel pressurized with hydrogen. A toluene solution of catalyst was added to the reactor by nitrogen over pressure. The reactor was maintained at isothermal conditions throughout the run. Ethylene was admitted to the reactor and controlled at 150 psi with feed on demand via a pressure regulator. After the reactor temperature and pressure stabilized, the catalyst slurry was charged into the reactor and polymerization initiated. Ethylene flow was monitored via a Brooks mass flow meter.

Polymerization was terminated by venting the reactor and the polymer recovered by filtration. The polymer was stabilized by the addition of about 1000 ppm of butylated hydroxytoluene/hexane (BHT) and further devolatilized 2 hours at 80° C. in a vacuum oven. Melt flow properties of the polymer were determined in accordance with ASTM D-1238. Polymer densities were measured on compression molded samples in a density gradient column in accordance with ASTM D-1505 85.

The following table gives the reaction conditions.

    __________________________________________________________________________             Temp.      Co-Monomer                                                                            Catalyst                                                                            Molar Ratio                                                                           H2,                                                                               Reaction Time                         Run                                                                               Catalyst                                                                            (°C.)                                                                       Co-Monomer                                                                            (grams)                                                                               (mmoles)                                                                            Al/M   ΔP                                                                          (Min)                                 __________________________________________________________________________      1 I    80  None    0      9.5E-3                                                                             1897    0 15                                     2 I    80  None    0      4.7E-3                                                                             3795    0 15                                     3 I    80  None    0      4.7E-3                                                                             1897   20 15                                     4 I    80  None    0      4.7E-3                                                                             1897   50 10                                     5 I    80  Butene 20      4.7E-3                                                                             1897   20 15                                     6 II   80  None    0      9.0E-3                                                                             1001    0 60                                     7 III  80  Butene 10      8.4E-3                                                                             1074   10 30                                     8 III  80  None   10      8.4E-3                                                                             1074   10 30                                     9 IV   80  Butene  0      6.6E-3                                                                             1324    0 30                                    10 IV   80  Butene 10      6.6E-3                                                                             1324   10 30                                     11*                                                                              V    80  Butene 10     1.14E-2                                                                             1175    0 10                                     12*                                                                              V    80  Butene 10     4.06E-3                                                                             1645    0 10                                     13*                                                                              V    80  Butene 10     8.12E-3                                                                             1645    0 10                                    14 VI   80  Butene 10     6.74E-3                                                                              991    0 15                                    15 VI   80  Butene 10     1.35E-2                                                                              991    0 15                                    16 VI   80  Butene 10     1.35E-2                                                                             1288    5 15                                    17 VI   80  Butene 10     1.89E-2                                                                             1132   15 15                                    18 VI   110 Butene 10     1.89E-2                                                                             1132    0 15                                    19 VII  80  Butene 10     1.10E-2                                                                             1212    0 15                                    20 VII  80  Butene 10     1.10E-2                                                                             1212    5 15                                    21 VII  110 Butene 10     1.54E-2                                                                             1126   15 15                                    22 VII  80  Butene 10     1.54E-2                                                                             1126    0 15                                    23 VII  80  Butene 10     1.54E-2                                                                             2078    0 15                                    __________________________________________________________________________      In the table, "Al/M" is ratio of moles of aluminum in PMAO to moles of         metal (titanium or zirconium) in the catalyst.                                 *Comparative Example                                                     

    ______________________________________                                         The following table gives the result of the polymerizations.                        Catalyst                                                                       Productivity                          Mw/                                 Run  (kg/gM/h)  MI2     MI20  MFR   Density                                                                               Mn                                  ______________________________________                                          1   179.0      <0.01   <0.01 --                                                2   153.2      <0.01   <0.01 --                                                3   165.5      <0.01   1.8   --                                                4   133.1      <0.01   2.47  --                                                5   272.9      <0.01   0.964 --                                                6    62.9      <0.01   <0.01 --                                                7    99.2      0.90    16.9  18.9  0.9513 2.51                                 8   167.9      0.41    4.2   10.2         3.67                                 9   103.2      <0.01   --    --                                               10    24.8      <0.01   --    --                                                11* low        --      --    --                                                12* one        --      --    --                                                13* none       --      --    --                                               14   none       --      --    --                                               15    98.1      <0.01   1.15  --                                               16   177.7      0.93    21.4  23.1                                             17   137.6      1.31    34.5  26.3                                             18   159.0      0.81    16.1  19.8                                             19   119.8      <0.01   .83   --                                               20   198.7      0.46    11.4  24.7                                             21   157.8      0.63    17.8  28.2                                             22   160.1      0.06    12.8  --                                               23   112.1      0.06    1.84  29.7                                             ______________________________________                                          *Comparative Example                                                     

In the table, kg/gm/h is kilograms polymer produced per gram of catalyst per hour. The melt index of the polymer was measured according to ASTM D-1238, Condition E and Condition F. MI2 is the melt index measured with a 2.16 kg weight (Condition E). MI20 is the melt index measured with a 21.6 kg weight (Condition F). MFR is the ratio of MI20 to MI2. The polymer density was measured according to ASTM D-1505. The molecular weight distribution of the polymer was measured using a Waters 150C gel permeation chromatograph at 135° C. with 1,2,4-dichlorobenzene as the solvent. Both weight average molecular weight (Mw) and the ratio of Mw to Mn (number average molecular weight) are used to characterize the molecular weight distribution.

The catalysts of this invention gave good productivities and high molecular weight polymers, as evidenced by very low MI values, and Catalysts VI and VII did so even at higher temperatures (110° C.). 

We claim:
 1. A method of making a poly-α-olefin comprising polymerizing an α-olefin monomer by contacting said α-olefin monomer in the presence of a cocatalyst with a catalyst that has the general formula ##STR18## where Y is O, S, NR, ##STR19## each R is independently selected from the group consisting of hydrogen and C₁ to C₆ alkyl, M is titanium, zirconium, or hafnium, each X is independently selected from the group consisting of halogen, C₁ to C₆ alkyl, C₁ to C₆ alkoxy, and ##STR20## L is X, cyclopentadienyl, C₁ to C₆ alkyl substituted cyclopentadienyl, indenyl, fluorenyl, or ##STR21## each R' is independently selected from the group consisting of R, C₁ to C₆ alkoxy, C₆ to C₁₆ aryl, halogen, and CF₃, and each "n" is 1 to
 4. 2. A method according to claim 1 wherein said catalyst has the general formula ##STR22##
 3. A method according to claim 2 wherein Y is oxygen and X is halogen.
 4. A method according to claim 2 wherein M is titanium.
 5. A method according to claim 2 wherein M is zirconium.
 6. A method according to claim 5 wherein Y is oxygen and X is halogen.
 7. A method according to claim 6 wherein X is chlorine.
 8. A method according to claim 7 wherein L is cyclopentadienyl.
 9. A method according to claim 8 wherein R' is selected from the group consisting of chlorine, methyl, and mixtures thereof.
 10. A method according to claim 1 wherein said catalyst is selected from the group consisting of 8-quinolinoxy-titanium trichloride, 8-(2-methyl-5,7-dichloro-quinolin)oxytitanium trichloride, (cyclopentadienyl)-(8-quinolinoxy)zirconium dichloride, (cyclopentadienyl)-[8-(2-methyl-5,7-dichloroquinolin)oxy]zirconiumdichloride, and mixtures thereof.
 11. A method of making a poly-α-olefin comprising polymerizing an α-olefin monomer by contacting said α-olefin monomer in the presence of a cocatalyst with a catalyst that has the general formula ##STR23## where Y is O, S, NR ##STR24## each R is independently selected from the group consisting of hydrogen and C₁ to C₆ alkyl, M is titanium, zirconium, or hafnium, each X is independently selected from the group consisting of halogen, C₁ to C₆ alkyl, C₁ to C₆ alkoxy, and ##STR25## L is X, cyclopentadienyl, C₁ to C₆ alkyl substituted cyclopentadienyl, indenyl, fluorenyl, or ##STR26## each R' is independently selected from the group consisting of R, C₁ to C₆ alkoxy, C₆ to C₁₆ aryl, halogen, and CF₃, and each "n" is 1 to
 4. 12. A method according to claim 11 wherein said catalyst is selected from the group consisting of bis(2-pyridinoxy)titanium dichloride, (cyclopentadienyl)(2-pyridinoxy)titanium dichloride, and mixtures thereof.
 13. A method according to claim 11 wherein Y is oxygen and X is halogen.
 14. A method according to claim 11 wherein M is titanium.
 15. A method according to claim 11 wherein M is zirconium.
 16. A method according to claim 15 wherein Y is oxygen and X is halogen.
 17. A method according to claim 16 wherein X is chlorine.
 18. A method according to claim 17 wherein L is cyclopentadienyl.
 19. A method according to claim 18 wherein R' is selected from the group consisting of chlorine, methyl, and mixtures thereof.
 20. A method of making a poly-α-olefin comprising polymerizing an α-olefin monomer by contacting said α-olefin monomer under polymerizing conditions in the presence of a methylaluminoxane cocatalyst with a catalyst that has the general formula ##STR27## where M is titanium or zirconium, X is halogen, L is halogen or cyclopentadienyl, and each R' is independently selected from the group consisting of hydrogen chlorine, methyl, and mixtures thereof. 